• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    1502045 Preparation of ethyibenzene hydroperoxide HALCON INTERNATIONAL Inc 21 April 1976 [21 April 1975] 16164/76 Heading C2C A process for the preparation of ethylbenzene hydroperoxide by liquid phase molecular oxygen oxidation of ethylbenzene comprises introducing liquid ethylbenzene and molecular oxygen into a reaction zone and withdrawing a liquid stream containing the hydroperoxide from said zone, removing vapours containing non-condensible inert gases from said reaction zone, separating condensible components from said vapours and regulating the reaction temperature within said zone by controlled recycle of said non-condensible gases to said zone. In one preferred embodiment of the invention, the liquid ethylbenzene is introduced into the first of a plurality of reaction zones connected together in series and the liquid stream containing the hydroperoxide is withdrawn from the last of said zones, vapours containing non-condensible inert gases are removed from each of said zones, and the reaction temperature within at least one of said zones is regulated by controlled recycle of said non-condensible gases to said zones. The hydroperoxides obtained by the present process may be reacted with olefins in the presence of a catalyst to produce epoxides, particularly propylene oxide.
    公开号:SU988189A3
    申请号:SU762346055
    申请日:1976-04-20
    公开日:1983-01-07
    发明作者:П.Шмидт Джон
    申请人:Халкон Рисерч Энд Дивелопмент Корпорейшн (Фирма)；
    IPC主号:
    专利说明:

    (5) METHOD FOR PRODUCING ETHYLBENZENE HYDROXIDE
    The invention relates to methods for producing ethylbenzene hydroperoxide which finds important applications in various chemical processes, for example, in epoxidation of propylene 5 to produce propylene oxide.
    A method of producing ethylbenzene hydroperoxide is known by oxidizing ethylbenzene with molecular oxygen.
    The oxidation of ethylbenzene in hydroperoxide of ethylbenzene is carried out at a gradually decreasing temperature in the range of lOO-lBo C. The process is carried out in an apparatus having several distinct oxidation zones, in such a way that the temperature will drop from zone in the direction of fluid flow.
    The spent oxygen-containing gas without contact with ethylbenzene is removed from the apparatus. The yield of the target product is 70-75% Li.
    The disadvantage of this method is the low yield of the target product.
    The purpose of the invention is to develop an oxide and ethylbenzene process in ethylbenzene hydroperoxide, ensuring a high yield of the target product and simplifying the process technology.
    The goal is achieved according to the method of producing ethylbenzene hydroperoxide by liquid-phase oxidation of ethylbenzene with oxygen-containing gas in successive oxidation zones at 100-180 ° C with the removal of vapor and liquid phases in which liquid ethylbenzene is brought the condensable components are separated from the vapors, and non-condensable gases contained in the vapor phase are recycled to the reaction zone.
    In addition, ethylbenzene is introduced into the first oxidation zone, and non-condensable gases are recycled to all OR (part of the oxidation zones. 398 The method allows to obtain the target product with output 88 and achieve significant energy savings. Figures 1 and 2 show recycling systems gas, Example 1. Ethylbenzene is oxidized with molecular oxygen to ethylbenzene hydroperoxide using the gas recycling system according to Fig. 1. The vapor along line 1 passes into condenser 2, and then into separator 3. Water condensate is drained from this separator and condensed The ethylbenzene, separated from the aqueous phase, is recycled to oxidation through line C. Discondensed vapors from the separator through line 5 are recycled through lines 6 and 7 to the reaction zone to provide the required temperature control, sufficient purging with unclinched vapors is carried out through 8 dl Compensation of these materials entering with the air introduced by line 9- The oxidation is carried out continuously using eight stages of oxidation 10-17. The mixture oxidized in the liquid phase in vase 10 is maintained at C, the mixture in zone 11 is maintained at 144 ° C, in zone 12 - at, in zone 13 at, in the zone at T38 ° C, in zone 15 - at, in zone 1b - at, and in zone 17 - at 132 ° C. The vapor lines from each zone are connected by a common pipeline 1, and the pressure in each of the oxidation zones is maintained at about 2.32 kg / cm.
    Ethylbenzene, heated to about 148c in preheater 18, is fed along the line to the oxidation zone 10 at a rate of about 23 mol / h. Air, preheated to about 130 °, is fed to reactor 19 at a speed of about 79 mol / h along line 9 and distributed over several oxidation zones 10-17. The vapors from the oxidation zones are withdrawn along line .1 at a rate of about 192 mol / h, they have a molar composition: about% nitrogen, ethylbenzene and% oxygen, the rest is for water and organic products. After cooling these vapors to release condensable products and separating from non-condensable vapors and after removing the above purge gases, the resulting recycled gas is compressed and fed into the reactor 19 at a rate of about
    In the process described, 88 moles of ethylbenzene hydroperoxide per 100 moles of oxidizable ethylbenzene and 6.7 moles of acetophenone as a by-product per 100 moles of ethylbenzene hydroperoxide are obtained.
    权利要求:
    Claims (2)
    [1]
    PRI me R 2 (comparative). Ethylbenzene is oxidized by molecular oxygen to ethylbenzene hydroperoxide, but without the gas recyclization system of the invention described in Example 1 and shown in FIG. 1. The vapors pass through line 1 to condenser 2, 4. 1.7 mol / h via line 7 and are distributed between eight oxidation zones. The molar composition of this recycle gas is as follows: about 97 nitrogen, 2% oxygen and 1 ethyl benzene. Condensed ethylbenzene is removed from separator 3 via line 20 and fed through line 21 to recycling. The liquid stream from the last oxidation zone 17 contains about 9.5 mol. % (12 wt.) Ethylbenzene hydroperoxide and 89 mol. % ethylbenzene, the rest is organic by-products. This mixture is distilled at a bottom temperature of about 80 ° C and about 50 of the ethylbenzene contained in it is removed, which is recycled to oxidation. The remainder of ethylbenzene is isolated in a post-treatment to recycle to oxidation. The distribution of air and the inert gas being recycled between the eight oxidation zones (the recycled gas is calculated from the free ethylbenzene) is presented in Table 1. Table 1 59 and then to separator 3. Condensate water and noncondensation (bath products are withdrawn from this separator, and condensed ethylbenzene is returned from the separator for line oxidation. Oxidation is carried out continuously, using shown in Fig. 1. The liquid phase of the oxidized mixture in zone 10 is maintained at, in zone 11 - at 10 in zone - at, in zone 13 at, in zone I - at 138 ° C, in zone 15 at 13b ° C, in zone 16 — at and in zone 17 — at 132 ° C. The temperature control is carried out with the help of cooling coils provided in each Tseke., taken along the lines from each zone, are collected in the common pipeline 1, the pressure in each of the oxidation zones is maintained at about 2.32 kgf / cm®. Ethylbenzene, heated to approximately in the preheater 18, is fed through line k to oxidation zone 10 with a speed of about 205 mol / h. Air, which is preheated to about, is fed to reactor 19 at a speed of about 81.5 mol / h on line 9 and distributed into several oxidation zones 10-17, as indicated that the combined vapors from the oxidation zones are removed along line 1 at a rate of about 12 mol / h; they have the following The molar composition is about 52 nitrogen, 6% ethyl benzene and 1% oxygen, the rest is water and organic by-products. The vapors are cooled to remove condensables, as already noted. The air distribution over the eight oxidation zones is shown in table. 2. Table 2. Oxidation zones. I Air (mol / h) 9 The liquid stream leaving the last oxidation zone contains approximately 9.5 mol. % (12 wt.%) Of ethylbenzene hydroperoxide and 89 mol. % ethylbenzene, the rest is organic by-products. This mixture is distilled at a temperature in the cube of about 80 ° C and about 50% of the ethylbenzene contained in it is recovered and recycled for oxidation. The remainder of ethylbenzene is isolated in a post-treatment to recycle to oxidation. In this process, only 86 moles of ethylbenzene hydroperoxide per 100 moles of oxidized ethylbenzrl and 8.0 moles of lcetophenone as a by-product per 100 moles of ethylbenzene hydroperoxide are obtained. Example 3. The procedure described in Example 1 is carried out using an inert gas: for recycling to the oxidation zones in accordance with the invention, as indicated, but in this case the system shown in FIG. 2, so that the ethylbenzene feed is directly contacted with. oxidized vapors. Thus, ethylbenzene supplied via line 1 enters the upper part of contact zone 2, and oxidized vapors through line 3 passes into the lower part of contact zone 2 for countercurrent contact with ethylbenzene. The condensed and decanted aqueous phase is removed via line C, the cooled gases are removed via line 5 to recycle to oxidation after appropriate purification, and the heated ethylbenzene is fed to line 6 and sent to oxidation zone 7 after passing through a preheater 8. The working conditions are as described in example 1. When operating in this way, essentially the same results are obtained for ethylbenzene hydroperoxide and for the production of by-products, but the importance of efficiency and efficiency of the process is important. Thus, for the process in this example, it is required to supply only about 18,000 calories per gram-mole of ethylbenzene hydroperoxide to the preheater 8, whereas for comparison to preheater 8, it is required to supply respectively 108000kal per gram-mole according to the process of example 1. Claim 1 obtaining hydroperoxide tilbenzene by liquid phase oxidation 7. 988189 Neither ethylbenzene with oxygen-containing gas in successive oxidation zones at 100–18 ° C with the extraction of vapor and liquid phases, was done because, in order to increase the yield of the target product and simplify the process technology, liquid ethylbenzene was brought into contact before entering the oxidation zone with vapors removed from the reaction zone, the condensable components 10 are separated from the vapors, and non-condensable
    vapor gases contained in the vapor phase are ejected into the reaction zone ..
    [2]
    2. The method according to claim 1, wherein the ethylbenzene is introduced into the first oxidation zone, and the non-condensable gases are recycled to all or part of the oxidation zones.
    Sources of information taken into account in the examination
    1, US Patent No. H 59810, cl. 260-610, published. 19b9.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU988189A3|1983-01-07|Process for producing ethylben/zene hydroperoxide
    US4618709A|1986-10-21|Waste water treatment in the production of methacrylic acid
    EP1773748B1|2010-05-19|Method for producing |acrylic acid
    US4246203A|1981-01-20|Process for the production of a phenol and a carbonyl compound by the catalyzed decomposition of an aromatic hydroperoxide
    EP2981528B1|2016-11-30|Process for the preparation of 2,5-furan-dicarboxylic acid
    CS203917B2|1981-03-31|Process for continuous preparing propylenoxide
    US4554054A|1985-11-19|Methacrylic acid separation
    USRE31381E|1983-09-13|Process for the preparation of propylene oxide
    CA1152519A|1983-08-23|PROCESS FOR THE PREPARATION OF .epsilon.-CAPROLACTONE
    GB1589310A|1981-05-13|Continuous process for producing terephthalic acid
    EP1293505A1|2003-03-19|Process for the epoxidation of olefins
    EP0102642A1|1984-03-14|Process for purifying methacrylic acid
    KR20020084899A|2002-11-13|Process for producing methyl methacrylate
    US9975839B2|2018-05-22|Paraxylene extraction of purification mother liquor with heat integration
    JP2002322167A|2002-11-08|Method for preparing propylene oxide
    IL28384A|1971-03-24|Process for recovery of glycidol
    JP2002322164A|2002-11-08|Method for preparing propylene oxide
    GB2096601A|1982-10-20|Process for producing methacrylic acid
    KR20210096174A|2021-08-04|Purification of aqueous solutions containing formaldehyde and use of the purified solution in a process for producing acrylic acid
    US4162268A|1979-07-24|Process for preparing diacetylbenzene
    US5334771A|1994-08-02|Peroxidation of secondary carbon in alkanes and cycloalkanes
    JPH0782247A|1995-03-28|Preparation of tert-butyl-hydroperoxide-containing mixture
    US4088699A|1978-05-09|Production of aralkyl tertiary hydroperoxides
    SU671208A1|1988-02-15|Method of producing isoprene
    KR20080096687A|2008-10-31|Use of predehydration towers in an ethane oxidation to acetic acid/ethylene process
    同族专利:
    公开号 | 公开日
    JPS564549B2|1981-01-30|
    BE840918A|1976-10-20|
    NL172237B|1983-03-01|
    FR2308619A1|1976-11-19|
    FR2308619B1|1979-08-10|
    IT1058164B|1982-04-10|
    DE2617432A1|1976-11-04|
    AU1298176A|1977-10-20|
    BR7602423A|1976-10-19|
    NL7603846A|1976-10-25|
    DE2617432B2|1979-02-15|
    GB1502045A|1978-02-22|
    AU500738B2|1979-05-31|
    CA1071656A|1980-02-12|
    DE2617432C3|1979-10-31|
    ZA761760B|1977-10-26|
    NL172237C|1983-08-01|
    ES447195A1|1977-07-01|
    US4066706A|1978-01-03|
    JPS51128931A|1976-11-10|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2637772A|1948-07-07|1953-05-05|Rca Corp|Keyed automatic gain control|
    US3459810A|1965-12-30|1969-08-05|Halcon International Inc|Process for the preparation of ethylbenzene hydroperoxide|
    US3351635A|1966-03-14|1967-11-07|Halcon International Inc|Epoxidation process|
    FR1491518A|1966-06-30|1967-08-11|Rhone Poulenc Sa|Preparation of hydroperoxides|
    JPS4945383A|1972-09-09|1974-04-30|US4408081B1|1981-10-05|1986-05-13|
    US4556748A|1983-10-31|1985-12-03|The Dow Chemical Company|Process for producing alkylene glycols|
    US4950794A|1989-05-24|1990-08-21|Arco Chemical Technology, Inc.|Ethylbenzene oxidation|
    US5210354A|1992-05-08|1993-05-11|Arco Chemical Technology, L.P.|Propylene oxide-styrene monomer process|
    US5276235A|1993-02-19|1994-01-04|Arco Chemical Technology, L.P.|Residual stream upgrading in a propylene oxide-styrene monomer process|
    US5675055A|1995-10-04|1997-10-07|Arco Chemical Technology, L.P.|Acidification/extraction treatment of waste caustic stream|
    US5883268A|1997-10-23|1999-03-16|Arco Chemical Technology, L.P.|Process stream purification|
    US6512129B1|2002-01-23|2003-01-28|Arco Chemical Technology, L.P.|Epoxidation process|
    US6755979B2|2002-08-15|2004-06-29|Arco Chemical Technology, L.P.|Peroxide impurities removal|
    EP1520853B1|2003-09-24|2009-12-30|Repsol Quimica S.A.|Process for preparation of hydroperoxides|
    US7901128B2|2004-07-20|2011-03-08|Dow Global Technologies Llc|Tapered aperture multi-tee mixer|
    RU2007111730A|2004-09-01|2008-10-10|Шелл Интернэшнл Рисерч Маатсхаппий Б.В. |HORIZONTAL REACTOR RESERVOIR|
    JP2009512695A|2005-10-21|2009-03-26|グラクソグループリミテッド|Compound|
    US8017812B2|2006-11-13|2011-09-13|Shell Oil Company|Process for the liquid phase oxidation of ethylbenzene into ethylbenzene hydroperoxide|
    US8142661B2|2008-09-29|2012-03-27|Lyondell Chemical Technology, L.P.|Residual stream upgrading in a propylene oxide-styrene monomer process|
    NL2007874C2|2011-11-25|2013-05-28|Progression Industry B V|The application of chemical compounds presents a styrene production process in a fuel.|
    CN106554298B|2015-09-28|2019-04-23|万华化学集团股份有限公司|A kind of method that ethylbenzene oxidation prepares ethylbenzene hydroperoxide|
    RU2633362C2|2016-01-12|2017-10-12|федеральное государственное бюджетное образовательное учреждение высшего образования "Казанский национальный исследовательский технологический университет" |Method of producing ethylbenzene hydroperoxide|
    ES2897519T3|2017-02-03|2022-03-01|Lyondell Chemical Tech Lp|Upgrading of waste streams in a propylene oxide/styrene co-production process|
    EP3619183B1|2017-05-01|2021-09-01|Lyondell Chemical Technology, L.P.|By-product stream upgrading in a propylene oxide/styrene coproduction process|
    EP3412635B1|2017-06-08|2021-04-14|Lyondell Chemie Nederland B.V.|Wastewater treatment method|
    CN107930555B|2017-11-30|2021-04-20|万华化学集团股份有限公司|Multistage horizontal stirring airlift reactor for preparing ethylbenzene hydroperoxide and application|
    SG11202103672TA|2018-12-26|2021-05-28|Wanhua Chemical Group Co Ltd|Device and method for oxidizing organic substance|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/569,734|US4066706A|1975-04-21|1975-04-21|Preparation of ethylbenzene hydroperoxide|
    [返回顶部]